Apparatus for removal of acidic gases from gaseous atmospheres



Dec. 23, 1969 B. J. MAYLAND ET AL 3,485,743

APPARATUS FOR REMOVAL OF ACIDIC GASES FROM GASEOUS ATMOSPHERES Filed July 21, 1967 3 Sheets-Sheet 1 32 a E 3 Fiej E KOH K 60 KH C 03 STU/C'H/OMETE/C QUANTITIES /NCREAS/NG CO; //V SOLUTION lNVENTOR/S BERTRANDJMAVLAND AND RossrarJoun STEINBERGER,

Dec. 23, 1969 B. J. MAYLAND ET A 3,485,743

APFARATUS FOR REMOVAL OF ACIDIC GASES FROM GASEOUS ATMOSPHERES 3 Sheets-Sheet 2 I Filed July 21, 1967 FROM ABSORBER AQU EOUS KOHoRKI-ICQ;

EEGENEIZATED SOLUTION TO ABSORBER INVENTOR/S FROM ABSORBER MAKE-UP STEAM Beam/mo J. MAYLAND AND I IIIIIIIIIIIIIII I m M g Id/lw M F w W a I. la

J P L as REGENERATED K CO;+KOH-I-I O FIG.4

| I I I I I I I ROBERT JOHN STEINBERGER,

ATTORNEYS Dec. 23, 1969 B. J. MAYLAND ET AL 3,485,743

APPARATUS FOR REMOVAL OF ACIDIC GASES FROM GASEOUS ATMOSPHERES 3 Sheets-Sheet 5 Filed July 21, 1967 INVENTOR/S BEKI'RAND JMAYLAND AND Roserzrdouu STEINBERGER,

ATTORNEYS United States Patent 3,485,743 APPARATUS FOR REMOVAL OF ACIDllC GASES FROM GASEOUS ATMOSPHERES Bertrand J. Mayland, Jefferstown, and Robert John Steinberger, Middletown, Ky., assignors to Girdler Corporation, Louisville, Ky., a corporation of Ohio Continuation-impart of application Ser. No. 342,072, Feb. 3, 1964. This application July 21, 1967, Ser. No. 655,017

Int. Cl. B011: 3/10, 1/00 US. Cl. 204234 3 Claims ABSTRACT OF THE DISCLOSURE An apparatus for the removal of acidic gases such as carbon dioxide and the like from gaseous atmospheres and process gases including an absorption tower wherein gases to be scrubbed are brought into intimate contact with an absorber solution containing an alkali metal carbonate and an alkali metal hydroxide and a regeneration system for regenerating the absorber solution by e'lectrodialysis.

CROSS-REFERENCE TO RELATED APPLICATIONS This application is a continuation-in-part of the copending application in the name of the same inventors, Ser. No. 342,072, filed Feb. 3, 1964, now US. Patent No. 3,344,050, and entitled, The Removal of Carbon Dioxide From Gaseous Atmospheres.

BACKGROUND OF THE INVENTION Field of invention The invention relates to apparatus for the removal of acidic gases such as carbon dioxide and the like from gaseous atmospheres, process gases and the like, and more particularly to an acidic gas stripping system characterized by apparatus which is small, compact and capable of high rates of absorption.

Description of the prior art In the chemical arts it is often desired to remove carbon dioxide, hydrogen sulfide, hydrogen cyanide, or other acidic gases from process gases and the like. This is usually accomplished by scrubbing the gases in a suitable tower with a water solution of a reagent capable of reacting with the acidic gases. Potassium carbonate is frequently used. For example, it reacts With carbon dioxide to form potassium bicarbonate in solution, which may be regenerated by driving off the excess carbon dioxide and either venting it or collecting it from some other usage.

Another type of solution frequently employed for scrubbing the gases is a solution containing an ethanolamine. Such a solution can also be regenerated.

In a copending application of Bertrand J. Mayland, one of the inventors herein, Ser. No. 104,559, filed Apr. 21, 1961, and entitled, The Removal of Carbon Dioxide From Gaseous Mixtures (now Patent No. 3,144,301, issued Aug. 11, 1964), it is taught, inter alia, that the addition of a small quantity of ethanolamine, such as monoethanolamine or diethanolamine, to a solution of potassium carbonate, increases the efficiency of the absorption or stripping system.

Various acidic gas removal systems have been devised which are capable of removing the gaseous constituent to various final levels in the treated process gases. It is a primary object of this invention to provide a process and apparatus for the general purposes described which is compact and efficient, requiring comparatively small apparatus.

3,485,743 Patented Dec. 23, 1969 "ice One of the uses for an acidic gas stripping system is the purification of air in submarines. Here the requirements are stringent. Space is at a premium, and it is necessary that the apparatus used be of small size. The acidic gas (primarily carbon dioxide in such an instance) content of the treated atmosphere must be reduced to a very low level. The treated atmosphere must also be free of fumes which would produce odors or toxic effects; and this immediately rules out the use of organic stripping materials such as the ethanolamines. This invention will be described in connection With an apparatus and process suitable for use in the removal of carbon dioxide from the atmosphere in a submarine or other restricted space such as a fallout shelter. It will be understood, however, that the principles of the invention can equally well be applied to the removal of other acidic gases and to commercial uses such as the treatment of process gases, with savings in equipment, cost of operation and efiiciency.

Other objects of the invention include the provision of a stripping solution which is essentially free of volatile materials excepting water, so that the treated atmosphere will not be contaminated, the provision of apparatus which is small and compact, the provision of a system with high rates of absorption, and the provision of a systern having reasonable energy requirements.

These and other objects of the invention which will be setforth hereinafter or will be apparent to one skilled in the art upon reading these specifications, are accomplished in that process and apparatus combination of which the aforesaid exemplary embodiment will now be described.

SUMMARY OF THE INVENTION The invention relates to the discovery that a system for the removal of carbon dioxide or other acidic gases from gaseous atmospheres or process gases utilizing (1) an absorber means with an absorber solution containing an alkali metal carbonate and an alkali metal hydroxide and (2) an electrodialysis regeneration system for the spent absorber solution, is characterized by high efficiency and minimum space requirements.

In an exemplary embodiment of the invention an absorber tower of comparatively small dimensions is provided wherein air containing a greater than desired quantity of carbon dioxide is scrubbed by a Water solution of potassium carbonate containing a small amount of free potassium hydroxide. The scrubbed air is carried by a conduit to cooling means and means for treating it with oxygen, if desired.

Means are provided for conducting spent absorber solution from the absorber tower to an electrolytic cell having a cathode and an anode of suitable inert electroconductive material. The cell is divided by an anion exchange membrane. The spent absorber solution is introduced into the cathode chamber and any suitable acid electrolyte is maintained in the anode chamber. Additional means are provided for cooling the regenerated absorber solution and conducting it from the cell to the absorber tower for rinse. The electrodialysis results in evolution of hydrogen at the cathode and a mixture of carbon dioxide and oxygen at the anode.

Separator means may be provided for each cell chamber to separate the generated gases from the electrolytes in the cell chambers or to separate entrained electrolyte droplets from the gases.

In another embodiment of the invention of the electrolytic cell is divided into three compartments by an anion exchange membrane and a cation exchange membrane. The first compartment contains a cathode and the spent absorber solution is introduced therein. The first compartment is separated from the second by the anion exchange membrane. The second chamber contains an aqueous potassium bicarbonate and is separated from the third compartment by the cation exchange membrane. The third compartment contains a suitable electrolyte such as aqueous sulfuric acid solution and the anode. In this embodiment hydrogen, carbon dioxide and oxygen may be separately derived and collected or vented. Means may be provided to circulate some of the hydrogen back to the second compartment to aid in gas stripping.

A third embodiment utilizes a cell similar to that of the second embodiment but divided into a plurality of chambers by ion exchange membranes. Means are provided for introducing spent absorber solution into appropriate ones of the chambers and removing regenerated solution therefrom. Additional means are provided for collecting or venting hydrogen, carbon dioxide and oxygen from the appropriate chambers.

BRIEF DESCRIPTION OF THE DRAWINGS FIG. 1 is a chart indicating the vapor pressure relationships of water and carbon dioxide in connection with solutions of potassium-bearing absorbing substances.

FIG. 2 is a diagrammatic representation of a simple absorption and regeneration system employing the principles of the invention.

FIG. 3 is a diagrammatic representation of a more elaborate form of electrodialysis cell.

FIG. 4 is a diagrammatic representation of an electrolytic means employing multiple cell regeneration.

FIG. 5 is a partial exploded view of a specific form of electrolytic cell useful in practicing the invention.

DESCRIPTION OF THE PREFERRED EMBODIMENTS As has been indicated, a solution of potassium carbonate, when used in a scrubber or absorber tower, can be regenerated when spent by the use of heat. But a solution of potassium carbonate has comparatively low absorption efiiciency, which requires the use of apparatus of considerable bulk and cost. It has been known, of course, that a solution of potassium hydroxide is a relatively eflicient absorption medium for carbon dioxide; but such a solution, when spent, cannot be regenerated in the same way as can a solution containing potassium bicarbonate. The present invention is based upon the discovery that the efliciency of absorption of a potassium carbonate solution can be very greatly increased by the addition of a relatively small quantity of potassium hydroxide, and upon the use of electrolytic means as a regeneration system for driving off carbon dioxide and regenerating potassium hydroxide. These factors permit the use of very small and compact apparatus, the overall volume reduction being of the order of to 50% as compared with an absorption apparatus using a solution of potassium carbonate alone. While reference is made herein to potassium carbonate and potassium hydroxide as the preferred materials, it will be understood that the carbonates and hydroxides of sodium or other alkali metals or mixtures thereof with potassium compounds may be employed.

Potassium carbonate, as has been indicated, has a relatively slow rate of absorption, so that at normal or room temperatures excessively large absorption towers or columns are required for a given carbon dioxide duty. The rates of absorption can be improved by the use of elevated temperatures, but this is expensive and, under some circumstances, inconvenient. Another disadvantage is the relatively high carbon dioxide vapor pressure of the conventionally regenerated solution, which is especially troublesome when the absorption is carried out at elevated temperatures to increase the rate of reaction. Thus, the conventional system is best for treating gases having a high carbon dioxide partial pressure arising either from a high content of carbon dioxide or from elevated pressure levels. Another disadvantage lies in the relatively high energy required for regeneration.

Potassium hydroxide reacts directly with carbon dioxide to form potassium carbonate. Potassium carbonate in the presence of water will react with carbon dioxide to form potassium bicarbonate or potassium acid carbonate. The first of these reactions is not reversible. Hence, the solution of potassium carbonate has negligible carbon dioxide vapor pressure. The second reaction is reversible. The solution will have a carbon dioxide vapor pressure increasing with the content of potassium bicarbonate.

Theserelationships are shown diagrammatically in FIG.-

1 where the carbon dioxide vapor pressure is plotted against increasing amounts of carbon dioxide in the solution. FIG. 1 also shows that the vapor pressure of water drops off gradually with an increasing content of carbon dioxide in the solution. This occurs because of the depressing elfect of the higher ion concentration; and it introduces a limitation on the energy efiiciency which can be obtained in conventional regeneration. Water will be stripped from the potassium bicarbonate solution along with carbon dioxide.

Considerable studies have been made of the action of additives to sodium carbonate solutions for absorption and subsequent stripping. These additives include the ethanolamines and other organic agents such as sucrose and various compounds of arsenic, tellurium, selenium and the like. For purposes of this invention in the exemplary usage, such additives should be avoided for obvious reasons. In other usages, however, such as the commercial treatment of process gases, additives may be employed if desired In the practice of this invention, it has been found that the use of a small amount of free hydroxide is as effective as or more etfective than most other additives in increasing the efficiency of absorption. This is shown in the following Table I which contrasts the use of sodium carbonate solutions with and without ethanolamine additives and with and without free hydroxide.

TABLE I.FEED 92.91% N 7.09% 002 Outlet,

Temp, Rate, Percent Solution F. cc./min. 002

18.99% KzCOa, 1.52% KOH 154 305 0.27 22.22% K1003, 0.54% KHCO 146 305 1.14 19.14% K1CO3, 0.27% KHCOa 106 150 l. 16 4% K2003 I50 3. 42 16.4% K2003 75 305 3. 50 11.73% K2003, 4.45% KOH 75 305 .45 14.21% K1003, 2.35% KOH 75 305 81 15.0% MEA,2.64 s.c.t. Cor/gal 75 305 19 32.8% MEA 6.438 s.c.i. COz/g 75 305 .56 26.0% KzCO; 75 305 3. 61 24.84% K200 2.96% KOH 75 305 0.1 27.48% K2003, 0.94% KOH" 75 305 0. l 27.93% K2003, 0.58% KOH- 75 305 0.8 28.57% K2003, 0.12% KOH 75 305 1. 40 15.0% DEA, 1.72 S.c.f. O0z/gal. 75 305 2. 24 30.0% DEA, 3.15 s.c.i. COz/gal 75 305 1. 4

l Operating concentration in a recent submarine unit test.

In the above table, MBA and DEA indicate respectively monoethanolamine and diethanolamine.

It will be seen, for example, that at F. a potassium carbonate solution of 18% to 20% concentration and containing from 1% to 2% potassium hydroxide does a betttr absorption job than the partially converted MEA solutions frequently used in submarine units. A potassium carbonate solution approaching 28% concentration with as little as 0.94% free hydroxide is much more effective even at room temperature.

The use of potassium carbonate solution containing free hydroxide as an absorption medium implies the use of a regeneration system capable of releasing carbon dioxide and of regenerating the hydroxide. This may be done electrolytically; but the use of a simple electrolytic cell is not feasible because, among other disadvantages, such a cell would release a gaseous mixture of carbon dioxide, hydrogen and oxygen. As a consequence, in the practice of this invention, recourse is had to electrodialysis which. even in its simplest form, results in the separate release of hydrogen from one compartment and the release of carbon dioxide and oxygen from the other.

Referring now to FIG. 2, which is diagrammatically illustrative of a simplified system suitable for use in a submarine, air containing a greater than desired quantity of carbon dioxide is delivered by a blower 1 to an absorber tower 2. In this tower, which contains a suitable packing or other means for bringing the air into intimate contact with the absorber solution, the air is scrubbed by means of a water solution of potassium carbonate containing a relatively small amount of free potassium hydroxide. The absorption efiiciency is high, and the carbon dioxide is reduced to a low level in a tower of comparatively small dimensions. The scrubbed air is shown issuing from the absorber at 3 where it is carried by a conduit to a cooling system. It will be understood that the air is treated with oxygen as may be required before being reintroduced into the living and operating spaces in the submarine.

The spent solution, which now contains potassium carbonate and potassium bicarbonate, collects in the bottom of the tower and is transferred by a pump 4 through a conduit 5 to an electrolytic cell 6. The transfer may be regulated by an automatic valve 7 in the conduit 5 and having connection with the sump in the bottom of the absorber tower.

A suitable construction for the electrolytic cell will later be described. However, it will be noted from FIG. 2 that the cell has a cathode 8 and an anode 9 of carbon or other suitably inert electro-conductive material. It will also be noted that the cell is divided into compartments 10 and 11 by an anion exchange membrane 12. An anion exchange membrane is generally a pervious support coated with an anion exchange resin. Anion exchange resins are generally in the free base (sometimes called hydroxyl) form, a example of which is chloromethylated styrene divinyl benzene copolymer, aminated with trimethylamine. Amberlite IR-410, Amberlite lR-40l, Amberlite IR45, Amberlite IR-400, and Amberlite IRA-410 are trademarks for resins of this class, and are suitable anion resins.

The result of the electrodialysis carried on in the cell 6 is the separate evolution of hydrogen at the cathode in compartment 10 and of a mixture of carbon dioxide and oxygen in compartment 11 at the anode 9, together with the reconversion of potassium bicarbonate to potassium carbonate and the regeneration of potassium hydroxide. The regenerated solution from the electrolytic cell, which generally will have been raised in temperature during the electrodialysis, may be reduced in temperature by a cooler 13 and transferred by a conduit 14. to the top of the absorber tower for reuse as shown. With solutions of the class hereinabove set forth, absorption may be carried on to advantage at a slightly elevated temperature, say about 180 F. It will be understood that a pump may be used in the conduit 14.

The hydrogen and the mixture of carbon dioxide and oxygen can be separately vented to the outside of the submarine without danger. The origin of the hydrogen and oxygen is, of course, the decomposition of water during the electrodialysis. Water make-up will be practiced as required. The solution to be regenerated is confined to compartment 10. Compartment 11 contains any suitable acid electrolyte.

The separation of the generated gases from the electrolytes in the cell chambers, or the separation of entrained electrolyte droplets from the gases, may require the use of conventional separators as indicated at 10a and 11a in FIG. 2. Although not illustrated therein, it will be understood that similar separators and flow circuits may be used with the cell compartments shown in FIGS. 3 and 4. In any flow circuits, pumps may be used to enforce circulation, whether or not shown in the drawings.

FIG. 3 illustrates diagrammatically a somewhat more elaborate electrolytic cell 15. This cell is divided into three compartments 16, 17 and 18 by an anion exchange membrane 19 and by a cation exchange membrane 20. A cation exchange membrane preferably comprises a foraminous support covered by a cation exchange resin so as to be impervious to the electrolyte. Cation resins are generally in a form which may be written RSO H, an example being a sulfonated divinyl benzene copolymer. Resins of this class are sold under trademarks such as Amberlite IR-120, Amberlite IR-l22, Amberlite IR-124 and Amberlite IRC-SO.

The electrolytic cell 15 contains a cathode 21 in compartment 16 and an anode 22 in compartment 18, these electrodes being connected to a suitable source of power.

The spent solution from the absorber enters the compartment 16, as at 23, and is regenerated therein both as to its content of potassium carbonate and as to its content of potassium hydroxide by an electrolytic action above described. The regenerated stripping solution is withdrawn from compartment 16 through a conduit 24 and is returned by means of pump 25 and a conduit 26 to the absorber.

The second compartment 17 is marked as containing an aqueous potassium bicarbonate solution. Acid bicarbonate ions enter through the anion exchange membrane 19 while hydrogen ions enter through the cation exchange membrane 20. The chemical result is the formation of some water and the evolution of some carbon dioxide.

The third compartment 18 is shown as containing a suitable electrolyte, such as an aqueous sulfuric acid solution. Here the result of electrolysis will be the transfer of hydrogen ions through the membrane 20 and the evolution of oxygen at the cathode 22.

The arrangement shown in FIG. 3 has the advantage that the gases hydrogen, carbon dioxide and oxygen are separately derived and collected and may be used or vented separately. It is possible, if desired, to circulate some of the hydrogen back to the compartment 17 to raid in gas stripping.

The separate evolution of the several gases hydrogen, oxygen and carbon dioxide is in many instances highly desirable. Uncontaminated oxygen can, of course, be reintroduced into the breathing atmosphere of a submarine or a fallout shelter. Hydrogen can often be used as fuel in burners or fuel cells. Carbon dioxide can sometimes be vented from a submarine in gaseous form. Where this is not feasible, there are various alternatives. The carbon dioxide may be liquefied by cryogenic heat exchange with the oxygen supply of the submarine, and stored, Also it is possible to convert a mixture of hydrogen and carbon dioxide to the form of a liquid hydrocarbon by a Fischer- Tropsch type of reaction.

A still more elaborate electrolytic arrangement is shown in FIG. 4 as comprising a cell 27 divided into a series of compartments 28 to 36, which compartments are separated by anion exchange membranes indicated in dotted lines and cation exchange membranes indicated in solid lines. The solution from the absorber is delivered by a branched conduit system 37 to compartments 28, 31 and 34. The regenerated solution from these compartments is delivered by a branched conduit system 38 to the pump 39 by means of which it is returned to the absorber. Compartment 28 contains a cathode 40, while compartment 36 contains an anode 41.

The nature of the solutions in the other compartments will be clear from the description above. Carbon dioxide will be released in compartments 29, 32 and 35 and may be collected and vented by a branched conduit system 42. Hydrogen will be evolved from compartment 28. Conduit means 43 may be employed to recirculate the hydrogen, along with any other stripping gas or steam, the use of which is desired, entering the system through a conduit 44. The recirculated gas is conducted to compartments 29, 32 and 35 by a branched conduit 45. Make-up water may be introduced into compartments 30, 33 and 36 through a branched conduit system 46. Oxygen can be vented from the system at 47. The actions going on in several compartments will be clear from the explanation above.

The reactions carried on in the electrolytic regenerator would result in /1 mol of oxygen with every mol of CO at the anode and /2 mol of hydrogen at the cathode. The theoretical electrical quantity for this would be one Faradays or 96493 coulombs/ gm. mol of C The net reaction is the decomposition of water. The theoretical electrical energy then is the standard free energy of this reaction, H O=H /2O This amounts to 99,000 B.t.u./1b. mol of H 0 or in terms of C0 130 B.t.u./s.c.f. of CO FIG. 5 illustrates a simple form of electrolytic apparatus which is not only self-contained, but will be non-spilling. The apparatus consists in a first end closure plate 48. Against this there will be placed a hollowed insulative element 49, preferably of resinous substance so as to form a cell compartment which will be closed upon the one side by the insulative plate 48, and on the other side by an ion exchange membrane 50. The first cell or compartment will contain a cathode 51 shaped to fit within the compartment, being made of any suitable conductive substance, :and having a electrical lead 52. The hollowed insulative member 49 is shown as provided with a plurality of fluid inlets or outlets 53, 54 and 55, together with a hole 56 for the passage of the lead 52.

The next element will be another hollowed insulative element 57 which, in the completed structure, will be covered on one side with the ion exchange membrane 50, and on the other side with an ion exchange membrane 58. A third hollowed insulative member is indicated at 59 and a final closure plate 60, also indicated; but it will be understood by the skilled worker in the art that while FIG. 5 shows the elements of a 3-compartment cell, these elements may be multiplied by any number required to make up a cell having more compartments, such as that illustrated in FIG. 4.

Any of the hollowed insulative elements may be provided with inlet and outlet openings, as required for the particular chemical changes going on in the particular com partment. These have not been illustrated excepting in the case of the hollow member 49. Also, it will be understood that if the hollow member 59 is used to form the last compartment in the cell construction, that construction will contain an anode (not shown) of the same general form and characteristics as the cathode 51 and its lead 52.

The several illustrated parts, excepting the electrodes, will be provided with holes 61 for the passage of bolts to hold all of the elements toe'gther in a liquidand gas-tight fashion. One of the bolts is illustrated at 60 in the figure. It will be understood that the several parts are intended to come into sealing relationship with each other; but the use of gaskets for sealing purposes does not depart from the spirit of the invention.

Modifications may be made in the invention without departing from the spirit of it.

We claims:

The embodiments of the invention in which an exclusive property or privilege is claimed are defined as follows:

1. A structure for removing acidic gases from gaseous atmospheres and process gases comprising an absorber tower, means for circulating an atmosphere through the absorber tower, means for circulating in counter-flow through the absorber tower a stripping solution for the acid gases comprising an alkali metal carbonate and an alkali metal hydroxide, an electrolytic device comprising a vessel divided into a first compartment and a second compartment by an anion exchange membrane, means for withdrawing solution from said absorber tower and circulating it as an electrolyte through the first of said compartments and returning it to the absorber tower, and means for maintaining circulation of a separate electrolyte in the said second compartment.

2. The structure claimed in claim 1 wherein the said vessel has a third compartment divided from the second compartment by a cation exchange membrane, the said first compartment containing a cathode and the said third compartment containing an anode and means for maintaining circulation of a separate electrolyte in said third compartment.

3. The structure claimed in claim 1 wherein said vessel is divided into a plurality of compartments divided respectively from each other by alternating anion exchange membranes and cation exchange membranes, one of the compartments in said vessel containing an anode and another compartment in said vessel containing a cathode, means for circulating solution from said absorber tower through certain of said compartments, and means for withdrawing from others of said compartments separate electrolytes therein and returning the electrolytes to the said compartments, and means in connection with said withdrawing and returning means for stripping gases from said several electrolytes.

References Cited UNITED STATES PATENTS 1,246,099 11/1917 Hulin 204234 XR 1,397,094 11/1921 Eustis 204234 XR 1,587,438 6/1926 Tainton 204-234 XR 1,875,310 8/1932 Youtz 204-234 XR JOHN H. MACK, Primary Examiner D. R. VALENTINE, Assistant Examiner US. Cl. X.R. 

